Olefin upgrading system for extracted feed

ABSTRACT

Apparatus is disclosed for oligomerizing olefinic Fischer-Tropsch liquids to produce heavier hydrocarbons by converting olefinic feedstock containing oxygenated hydrocarbons over an acidic zeolite catalyst. The improvement comprises an extraction unit for removing oxygenates from the feedstock; means for converting the extracted feedstock in a primary stage distillate mode catalytic reactor system under low severity conditions at high pressure and moderate pressure; means for recovering the oxygenates and light hydrocarbons from the primary stage and a secondary stage reactor system for conversion of oxygenates under high severity conditions at substantially higher temperature than the primary stage, thereby converting oxygenates and light hydrocarbons to heavier hydrocarbons.

CROSS REFERENCE TO COPENDING APPLICATION

This application is a continuation-in-part of copending U.S. patentapplication Ser. No. 600,699, filed Apr. 16, 1984, now U.S. Pat. No.4,513,156, incorporated herewith by reference.

FIELD OF INVENTION

This invention relates to a continuous system for converting olefinfeedstock to heavier hydrocarbons, especially for the manufacture ofdistillate range hydrocarbon fuels. In particular it provides apparatusfor operating an integrated two-stage MOGD type plant wherein anoligomerization catalyst, such as crystalline zeolite of the ZSM-5 type,is employed for converting olefinic feedstocks containing liquid alkenesand oxygenates at elevated temperature and pressure.

BACKGROUND OF THE INVENTION

Conversion of olefins to gasoline and/or distillate products isdisclosed in U.S. Pat. Nos. 3,960,978 and 4,021,502 (Givens, Plank andRosinski) wherein gaseous olefins in the range of ethylene to pentene,either alone or in admixture with paraffins are converted into anolefinic gasoline blending stock by contacting the olefins with acatalyst bed made up of a ZSM-5 type zeolite. In U.S. Pat. Nos.4,150,062 and 4,227,992 Garwood et al disclose the operating conditionsfor the Mobil Olefin to Gasoline Distillate (MOGD) process for selectiveconversion of C₃ ⁺ olefins.

The phenomena of shape-selective polymerization are discussed by Garwoodin ACS Symposium Series No. 218, Intrazeolite Chemistry, "Conversion ofC₂ -C₁₀ to Higher Olefins over Synthetic Zeolite ZSM-5", 1983 AmericanChemical Society.

Typically, the process recycles cooled light hydrocarbons from ahigh-temperature, high-pressure separator downstream of the catalyst bedback into the reaction zone where additional olefins are converted togasoline and distillate products. If the reaction of the olefins inconverting them to distillate and gasoline is allowed to progress in thecatalyst stream without any measures taken to prevent the accumulationof heat, the reaction becomes so exothermically accelerated as to resultin high temperatures and the production of undesired products.

In the process for catalytic conversion of olefins to heavierhydrocarbons by catalytic oligomerization using an acid crystallinezeolite, such as ZSM-5 type catalyst, process conditions can be variedto favor the formation of either gasoline or distillate range products.At moderate temperature and relatively high pressure, the conversionconditions favor distillate range product having a normal boiling pointof at least 165° C. (330° F.). Lower olefinic feedstocks containing C₂-C₆ alkenes may be converted selectively; however, the distillate modeconditions do not convert a major fraction of ethylene due to lowseverity conditions. While propene, butene-1 and others may be convertedto the extent of 50 to 95% in the distillate mode, only about 10 to 50%of the ethylene component will be consumed.

In the high severity or gasoline mode, ethylene and the other lowerolefins are catalytically oligomerized at higher temperature andmoderate pressure. Under these conditions ethylene conversion rate isgreatly increased and lower olefin oligomerization is nearly complete toproduce an olefinic gasoline comprising hexene, heptene, octene andother C₆ ⁺ hydrocarbons in good yield. To avoid excessive temperaturesin the exothermic reactors, the lower olefinic feed may be diluted. Inthe distillate mode operation, olefinic gasoline may be recycled andfurther oligomerized, as disclosed in U.S. Pat. Nos. 4,211,640 (Garwoodand Lee) and 4,433,185 (Tabak). The above cited publications areincorporated herein by reference.

One important source of olefinic feedstocks of interest for conversionto heavier fuel products is the intermediate olefin-rich light oil ornaphtha obtained from Fischer-Tropsch conversion of synthesis gas. Thesesynthol materials contain, in addition to olefins, a minor amount ofcoproduced oxygenated hydrocarbons. It has been found that theseoxygenates can interfere with catalytic oligomerization of olefins,particularly under the low severity conditions employed for makingdistillate and heavier hydrocarbons. It is an object of this inventionto overcome such catalytic deactivation by oxygenates, and to providemanufacturing methods and apparatus adapted to employ Fischer-Tropschliquid feedstocks.

SUMMARY

A process has been discovered for converting olefins to heavier liquidhydrocarbons comprising contacting an olefinic liquid hydrocarbonfeedstream containing oxygenated hydrocarbons with a polar solvent underliquid extraction conditions and recovering a polar extract phasecontaining the oxygenated hydrocarbons and an olefinic liquid raffinatestream substantially free of oxygenated hydrocarbons; contacting theolefinic liquid stream in a first catalyst reactor zone witholigomerization catalyst at elevated pressure and moderate temperatureunder conditions favorable for conversion of olefins to a first reactoreffluent stream rich in distillate range hydrocarbons; flashing thedistillate-rich stream and separating the first reactor effluent streaminto a liquid product stream rich in distillate and a vapor streamcontaining lower hydrocarbons; separating oxygenated hydrocarbons fromthe polar extract phase; and contacting at least a portion of the vaporstream from the flashing step and recovered oxygenated hydrocarbons in asecond catalyst reactor zone with oligomerization catalyst at moderatepressure and elevated temperature under conditions favorable forconversion of lower olefins and oxygenates to a second reactor effluentstream rich in heavier hydrocarbons. The process is particularly usefulwhere the olefinic feedstream is rich in C₃ ⁺ mono-olefins and containsa minor amount of C₂ -C₆ oxygenates. Advantageously the polar solventconsists essentially of water, and by-product water is recovered from atleast one reactor zone and recycled as extraction solvent.

In order to maximize distillate production the first and second effluentstreams may be fractionated to provide a gasoline-range hydrocarbonstream, and at least a portion of the gasoline stream is recycled to thefirst reactor zone.

THE DRAWINGS

FIG. 1 is a process flow sheet showing the major unit operations andhydrocarbon streams; and

FIG. 2 is a graphic plot of operating temperature and stream time forcomparative runs using two feedstocks.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

The oligomerization catalysts preferred for use herein include thecrystalline aluminosilicate zeolites having a silica to alumina ratio ofat least 12, a constraint index of about 1 to 12 and acid crackingactivity of about 160-200. Representative of the ZSM-5 type zeolites areZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35 and ZSM-38. ZSM-5 is disclosed andclaimed in U.S. Pat. No. 3,702,886 and U.S. Pat. No. Re. 29,948; ZSM-11is disclosed and claimed in U.S. Pat. No. 3,709,979. Also, see U.S. Pat,No. 3,832,449 for ZSM-12; U.S. Pat. No. 4,076,842 for ZSM-23; U.S. Pat.No. 4,016,245 for ZSM-35 and U.S. Pat. No. 4,046,839 for ZSM-38. Thedisclosures of these patents are incorporated herein by reference. Asuitable shape selective medium pore catalyst for fixed bed is a HZSM-5zeolite with alumina binder in the form of cylindrical extrudates ofabout 1-5 mm. Other pentasil catalysts which may be used in one or morereactor stages include a variety of medium pore (˜5 to 9 Å) siliceousmaterials such as borosilicates, ferrosilicates, and/or aluminosilicatesdisclosed in U.S. Pat. Nos. 4,414,143 and 4,417,088, incorporated hereinby reference.

The present invention is intended primarily for conversion of olefinicfeedstocks containing a major amount of naphtha range aliphatichydrocarbons in combination with a minor amount of oxygenatedhydrocarbons. Typically, the feedstock is rich in volatile C₃ -C₁₀liquid mono-olefins; however, more volatile and heavier hydrocarbons inthe C₂ -C₁₂ range may be present. The process is particularly welladapted to oligomerizing C₃ -C₇ olefins. Ethylene may be present to theextent it would be soluble in the liquid feedstock under processconditions.

Referring to the drawing, feedstock consisting essentially ofFischer-Tropsch naphtha fraction is introduced via feed conduit 1 to thebottom inlet of a continuous liquid-liquid extraction unit 10 wherein itis contacted in countercurrent flow operation with a polar solventintroduced via top solvent conduit 12 wherein makeup solvent (e.g.,water) is combined with a recycle stream 14, which may consistessentially of recycled polar solvent with a minor amount of residualoxygenate. The extraction unit 10 depicted is a stirred multi-stagevertical extraction column adapted for contiuous operation atsuperatmospheric pressure (e.g., about 600 to 1500 kPa). It isunderstood that any suitable extraction equipment may be employed,including cocurrent, cross-current or separate stage contactors, whereinthe liquid feedstock is intimately contacted with an immiscible solvent.This unit operation is described in Kirk-Othmer Encyclopedia of ChemicalTechnology (Third Ed.), 1980, pp. 672-721. The oxygenate extraction stepcan be carried out in any counter-current multistage design such as asimple packed column, rotating disk column, agitated column with bafflesor mesh, or a series of single stage mixers and settlers.

The heavier solvent phase, rich in oxyqenate solute, is recovered viabottom outlet 15 and may be further separated by decanting anyhydrocarbon phase carryover in separator 16 to be combined wih the mainnaphtha raffinate stream 17 exiting the extraction column 10 via anotherdecanting unit 18 before being pressurized by pumps 19. The extractedfeedstock is then heated at reaction pressure by passing sequentiallythrough reactor effluent heat exchangers 20C, B, A and furnace 21 priorto entering a series of fixed bed catalytic reactors 25A, B, Ccontaining the oligomerization catalyst. These reactors are preferablyoperated in the distillate mode to maximize production of C₁₀ +aliphatics. The cooled effluent from the last reactor 25C is flashed bypassing through pressure reduction valve 27 into a first hightemperature separator drum 30, from which a heavy hydrocarbon productrich in C₁₀ -C₂₀ distillate is recovered. Overhead vapor from separator30 is cooled by heat exchanger 32 and condensate is passed from secondlow temperature separator 34 to a liquid decanting unit 36 for recoveryof any byproduct water, which is recycled via conduit 38 and pump 39 torecycle line 14. The hydrocarbon phase from liquid decanting unit 36 isrecycled via pump 37 for combining with feedstock to the firstdistillate mode reactor stage. Overhead vapor from the second separator34 is passed via conduit 35 through heat exchanger 40 and furnace 42 tothe second reactor stage 45, which is operated under high severityconversion conditions at elevated temperature and reduced pressure, ascompared to the first stage. The increased temperature is sufficient tooligomerize unconverted light olefins from the first stage, even in thepresence of water. The second stage effluent stream, rich in gasolinerange hydrocarbons and other heavier hydrocarbons, is then cooled inexchanger 40 and passed to the recovery section. Condensed water may berecovered along with heavy liquid hydrocarbons from high temperatureseparator 46 and decanter 47. The gasoline-rich hydrocarbons may berecycled via pump 48 for combining with feedstock prior to the firststage. Overhead vapor from the secondary stage separator 46 may befurther cooled by exchanger 49 to obtain an offgas stream and C₃ -C₄rich in LGP product, a portion of which may be recycled to the secondarystage as a heat sink or diluent. Distillate and/or gasoline range heavyhydrocarbons may be recovered and fractionated separately from each ofthe main stages.

Fractionation of the distillate rich first stage product and gasolinerich second stage product streams may be effected in any suitablemanner, including the distillation technique disclosed in U.S. Pat. No.4,456,779 (Owens et al), incorporated herein by reference. Optionally, aportion of the gasoline range hydrocarbons from fractionation may becombined with feedstock prior to the first stage.

The water phase recovered from the extraction unit 10 may be recoveredand taken out of the system; however, it is preferred to recoveroxygenates for conversion under high severity conditions in thesecondary stage reactor. Advantageously, the oxygenate-rich extract ispassed via conduit 49 to distillation tower 50 where the volatileorganic compounds are stripped from the polar solvent. The overheadstream 52, which may contain water in addition to to oxygenates, iscombined with light olefinic gas from conduit 35 prior to the secondarystage. In general, it is advantageous to minimize the quantity of waterthe overhead stream from tower 50. However, where oxygenated compoundsare present which may boil close to the boiling point of water,carryover in conduit 52 may be as high as 5 parts water to 1 partoxygenates. Bottoms from tower 50 may be combined with byproduct waterand recycled via pump 39 and conduit 14 to the extraction unit.

It is advantageous to have the water travel in a closed loop so that anyhydrocarbons carried into the water phase during extraction do not needto be removed from the water. Excess water such as produced by oxygenatedehydration can be removed by any of several available purge lines.Also, since the second stage reactor 45 will dehydrate the oxygenates itwill act to remove oxygenates from the extraction loop while purifyingthe water phase.

The extraction unit may be operated from 0 to 100° C., preferably atambient temperature (20°-25° C.) and under pressure. While approximatelyequal amounts of water and feedstock are satisfactory, ,their ratios maybe varied widely (e.g., 10:1 to 1:10 parts by volume). Fischer-Tropschnaphtha (i.e. synthol light oil) typically contains about 2 to 15 wt %oxygenates. In one example herein a C₅ -C₆ olefinic feedstock isextracted in multiple stages to reduce the oxygenate content of theraffinate at substantially below 1 wt %.

In order to demonstrate the differences between unextracted feedstockscontaining oxygenates and oxygenate-free olefinic feedstock comparativeruns are made in a continuous process. Operating in the maximumdistillate mode under low severity conditions at moderate temperatureand high pressure, the runs are conducted for a period of seven days onstream, using a fixed bed of standard small crystal HZSM-5 extrudatecatalyst having an acid activity (α) of about 175 and containing 35%alumina binder. The process was operated at sufficient temperature toachieve essentially complete conversion of C₅ -C₆ olefins. Feedstockcomposition and process results are tabulated below for each feedstock.

                                      TABLE I                                     __________________________________________________________________________    C.sub.5 -C.sub.6 OLEFIN FEEDSTOCK*                                            OXYGENATE-FREE                                                                                     DAYS ON STREAM                                                                1   2   3   4   5   6   7                                __________________________________________________________________________    OPERATING CONDITIONS                                                          Ave. Reactor Temp., F.                                                                             399 399 405 406 409 412 420                              Pressure, psig       601 601 601 601 602 602 602                              LHSV (Total)         1.0 1.0 1.0 1.0 1.0 1.0 1.0                              LHSV (Olefin)        0.8 0.8 0.8 0.8 0.8 0.8 0.8                              TOTAL OLEFIN CONVERSION, WT %                                                                      100.00                                                                            99.99                                                                             100.00                                                                            99.98                                                                             99.86                                                                             99.84                                                                             99.89                            1-Pentene Conv., wt %                                                                              100.00                                                                            99.98                                                                             99.99                                                                             99.97                                                                             99.73                                                                             99.69                                                                             99.79                            1-Hexene Conv., wt % 100.00                                                                            100.00                                                                            100.00                                                                            100.00                                                                            100.00                                                                            100.00                                                                            100.00                           PRODUCT YIELDS (On conv. olefin)                                              C.sub.4.sup.-, wt %  0.78                                                                              0.67                                                                              0.27                                                                              0.54                                                                              3.01                                                                              0.14                                                                              0.42                             C.sub.5 -330F Gasoline, wt %                                                                       14.83                                                                             15.12                                                                             15.85                                                                             15.62                                                                             22.45                                                                             23.68                                                                             22.55                            330F+ Distillate, wt %                                                                             84.39                                                                             84.21                                                                             83.88                                                                             83.84                                                                             74.53                                                                             76.18                                                                             77.03                            GASOLINE, °API                                                                              77.4                                                                              76.7                                                                              76.3                                                                              76.2                                                                              75.0                                                                              74.6                                                                              75.0                             5 wt %, F            87  89  89  90  97  106 --                               50 wt %, F           164 164 165 177 159 166 --                               95 wt %, F           336 339 344 324 337 356 --                               DISTILLATE, °API                                                                            45.5                                                                              46.5                                                                              46.5                                                                              47.0                                                                              50.5                                                                              50.2                                                                              49.9                             5 wt %, F            326 323 321 319 315 312 319                              50 wt %, F           505 492 488 482 385 384 398                              95 wt %, F           767 734 733 724 634 642 650                              TLP 50% PT, F        405 387 390 385 345 345 347                              __________________________________________________________________________    *FEED COMPONENTS                                                                           Weight %                                                         1-Pentene    35.0                                                             1-Hexene     49.0                                                             N--Hexane    16.0                                                         

                                      TABLE II                                    __________________________________________________________________________    C.sub.5 -C.sub.6 OLEFIN FEEDSTOCK*                                            WITH 2.5 WT % OXYGENATES                                                                           DAYS ON STREAM                                                                1   2   3   4   5   6   7                                __________________________________________________________________________    OPERATING CONDITIONS                                                          Ave. Reactor Temp., F.                                                                             398 444 475 483 491 495 503                              Pressure, psig       605 607 615 600 600 602 601                              LHSV (Total)         1.0 1.0 0.9 1.0 1.0 1.0 1.0                              LHSV (Olefin)        0.8 0.8 0.8 0.9 0.8 0.8 0.8                              TOTAL OLEFIN CONVERSION, WT %                                                                      94.17                                                                             99.24                                                                             99.89                                                                             99.95                                                                             99.89                                                                             99.88                                                                             99.94                            1-Pentene Conv., wt %                                                                              92.56                                                                             98.82                                                                             99.77                                                                             99.90                                                                             99.77                                                                             99.74                                                                             99.87                            1-Hexene Conv., wt % 95.35                                                                             99.60                                                                             100.00                                                                            100.00                                                                            100.00                                                                            100.00                                                                            100.00                           PRODUCT YIELDS (On conv. olefin)                                              C.sub.4.sup.-, wt %  0.94                                                                              4.51                                                                              2.17                                                                              0.29                                                                              0.53                                                                              0.49                                                                              0.29                             C.sub.5 -330F Gasoline, wt %                                                                       91.45                                                                             31.98                                                                             25.27                                                                             21.35                                                                             19.98                                                                             21.45                                                                             26.90                            330F+ Distillate, wt %                                                                             7.61                                                                              63.51                                                                             72.56                                                                             78.37                                                                             79.59                                                                             78.06                                                                             72.81                            GASOLINE, API        79.4                                                                              73.8                                                                              73.8                                                                              73.1                                                                              73.3                                                                              73.4                                                                              73.0                             5 wt %, F            93  94  96  97  97  96  133                              50 wt %, F           157 159 161 162 162 161 264                              95 wt %, F           277 323 330 337 335 333 405                              DISTILLATE, API      43.5                                                                              49.7                                                                              47.3                                                                              47.3                                                                              47.2                                                                              47.7                                                                              47.55                            5 wt %, F            --  318 321 320 323 319 326                              50 wt %, F           --  406 475 473 480 460 477                              95 wt %, F           --  692 761 752 755 736 922                              TLP 50% PT, F        156 334 358 370 363 355 378                              WATER, wt % FEED     --  --  0.46                                                                              0.43                                                                              --  --  --                               OXYGEN, CONV. TO WATER, WT %                                                                       --  --  46.11                                                                             43.19                                                                             --  --  --                               __________________________________________________________________________    *FEED COMPONENTS                                                                           Weight %                                                         1-Pentene    40.8                                                             1-Hexene     42.2                                                             N--Hexane    14.5                                                             Acetaldehyde  0.3                                                             Methylethylketone                                                                           1.6                                                             Ethyl Acetate                                                                              trace                                                            1-Butanol     0.6                                                         

The data in Table I show a slight increase in operating temperature overthe seven day run, indicating high catalyst activity. A consistentlyhigh yield of distillate product is obtained, and it is noted that the50% boiling point for total liquid product (TLP) is also high,indicating heavy product. By contrast, the operating temperature forunextracted feed shown in Table II is increased at an average rate morethan five times that of the oxygenate-free feedstock. This difference incatalyst activity is depicted in FIG. 2, which is a plot of averageoperating temperature vs. time on stream.

The oxygenate-containing feedstock shown in Table II can be extracted atambient temperature with equal volumes of water. After two contactstages the acetaldehyde content is decreased to 0.01 wt % and 1-butanolto 0.03%. By employing several contact stages, a feedstock essentiallyfree of oxygenates can be obtained. A typical Fischer-Tropsch naphtha(C₅ -C₆ cut) contains trace amounts of C₃ ⁻ aliphatics, about 0.1 to 10%C₄ -C₅ aliphatics, 20-50% pentenes, 20-50% hexenes, along withsubstantial amounts of C₅ ⁻ saturates. The oxygenates may include C₂₋₄aldehydes, C₃₋₆ aliphatic alcohols, ketones, etc., typically boilingfrom about 20° to 120° C.

The polar solvents which may be employed in the extraction units havebeen exemplified by water; however, other suitable polar extractionsolvents may be employed within the inventive concept. For instance,organic compounds or mixtures thereof may be employed. Chemical andphysical properties of these extraction solvents are selected accordingto the particular feedstock hydrocarbon content and oxygenateimpurities.

For ease of operation under ambient conditions, especially in agravity-type countercurrent unit, a significant difference betweenraffinate phase and solvent is needed, usually at least 0.1 gm/cc.Advantageously, those extraction solvents having a specific gravitygreater than about 1.0 gm/cc are used. In addition, the lighterhydrocarbon liquid phase should be substantially immiscible with theheavier extraction solvent.

Polarity of the solvent may be expressed by reference to its dielectriccontent and dipole moment. Preferred organic solvents have a dielectricconstant greater than 20, say about 30 to 50; and a dipole momentgreater than about 0.6 Debye units.

For ease of recovering extracted oxygenates from the solvent bydistillation, it is preferred to have a higher boiling solvent having aboiling range at least about 30° C. above the extracted compounds.

Organic solvents having these properties include compounds havingcarbonyl, hydroxyl, amino, ether, nitro, halogen groups, etc., such aspropylene carbonate, monoethanolamine, furfural, dimethylsulfoxide andalkylene glycols.

It is understood by one skilled in the art that multiple extractionsteps can be employed such as water washing followed by organicextraction using one or more of the above compounds.

A typical distillate mode first stage reactor system is multi-reactorsystem, employed with inter-zone cooling, whereby the reaction exothermcan be carefully controlled to prevent excessive temperature above thenormal moderate range of about 190° to 315° (375°-600° F.).Advantageously, the maximum temperature differential across each lowseverity reactor is about 30° C. (ΔT˜50° F.) and the space velocity(LHSV based on olefin feed) is about 0.5 to 1.5. Heat exchangers provideinter-reactor cooling and reduce the effluent to flashing temperature.

Between stages it is preferred to take advantage of a significantpressure drop by flashing the effluent with a pressure differential ofat least 1400 kPa (200 psi) between the first stage and phase separatorvessel. By operating the first stage at elevated pressure of about 4200to 7000 kPa (600-1000 psig), this can be achieved. Preferably, adistillate mode reactor has sufficient total pressure to assure a totalolefin (feedstock plus recycle) partial pressure of at least about 3300kPa (500 psig).

The high severity second stage reactor is relatively simple, since thehigher temperature conversion does not require maximum differentialtemperature control closer than about 65° C. (ΔT˜20° F.) in theapproximate elevated range of 285° C. to 375° C. (550°-700° F.). Thereactor bed is maintained at a moderate super atmospheric pressure ofabout 400 to 3000 kPa (50-400 psig) and the space velocity for ZSM-5catalyst to convert oxygenates and light olefins should be about 0.5 to3 (LHSV). Preferably, all of the catalyst reactor zones in the systemcomprise a fixed bed down flow pressurized reactor having a porous bedof ZSM-5 type catalyst particles with an acid activity of about 160 to200.

Various modifications can be made to the system, especially in thechoice of equipment and non-critical processing steps. While theinvention has been described by specific examples, there is no intent tolimit the inventive concept as set forth in the following claims.

What is claimed is:
 1. A continuous system for converting olefins toheavier liquid hydrocarbons comprising(a) an extraction unit having ameans for contacting an olefinic liquid hydrocarbon feedstreamcontaining oxygenated hydrocarbons with a polar solvent under continuouscountercurrent liquid extraction conditions, and means for recovering apolar extract phase containing the oxygenated hydrocarbons and anolefinic liquid raffinate stream substantially free of oxygenatedhydrocarbons; (b) a first reactor including means for contacting theolefinic liquid raffinate stream in a first catalyst reactor zone witholigomerization catalyst at elevated pressure and moderate temperatureunder conditions favorable for conversion of olefins to a first reactoreffluent stream rich in distillate range hydrocarbons; (c) means forseparating the first reactor effluent stream into a liquid productstream rich in distillate and a vapor stream containing lowerhydrocarbons; (d) distillation means for separating oxygenatedhydrocarbons from the polar extract phase; and (e) a second reactorhaving means for contacting at least a portion of the vapor streamcontaining lower hydrocarbons and recovered oxygenated hydrocarbons in asecond catalyst reaction zone with oligomerization catalyst at moderatepressure and elevated temperature under conditions favorable forconversion of lower olefins and oxygenates to a second reactor effluentstream rich in heavier hydrocarbons.
 2. The system of claim 1 includingmeans for recovering byproduct water from at least one reactor zone forrecycle as extraction solvent.
 3. The system of claim 1 including meansfor fractionating the first and second effluent streams to provide agasoline-range hydrocarbons streams, and means for recycling at least aportion of the gasoline stream to the first reactor zone.
 4. The systemof claim 2 wherein the catalyst reaction zones comprise fixed bed downflow pressurized reactors having a porous bed of catalyst particles. 5.A reactor system for converting a Fischer-Tropsch liquid synthol rich inolefins to heavier liquid hydrocarbons comprisingextraction means forcontacting an olefinic liquid hydrocarbon feedstream containingoxygenated hydrocarbons with a polar solvent under liquid extractionconditions and recovering a polar extract phase containing theoxygenated hydrocarbons and an olefinic liquid raffinate streamsubstantially free of oxygenated hydrocarbons; first stage reactor meansfor contacting the olefinic liquid stream in a first catalyst reactorzone with shape selective oligomerization catalyst at elevated pressureand moderate temperature under conditions favorable for conversion ofolefins to a first reactor effluent stream rich in distillate rangehydrocarbons; phase separation means for flashing the distillate-richstream and separating the first reactor effluent stream into a liquidproduct stream rich in distillate and a vapor stream containing lowerhydrocarbons; distillation means for separating oxygenated hydrocarbonsfrom the polar extract phase; and second stage reactor means forcontacting at least a portion of the vapor stream from the phasesepartion means and recovered oxygenated hydrocarbons in a secondcatalyst reactor zone with shape selective oligomerization catalyst atmoderate pressure and elevated temperature under conditions favorablefor conversion of lower olefins and oxygenates to a second reactoreffluent stream rich in heavier hydrocarbons.
 6. The reactor system ofclaim 5 further comprising means for recovering byproduct water from atleast one reactor zone for recycle to the extraction means.
 7. Thereaction system of claim 5 further comprising fractionation means forseparating the first and second reactor stage effluent streams toprovide a gasoline range hydrocarbon stream and recycle means forcombining the gasoline stream with extracted feed to the first reactorstage.
 8. The reaction system of claim 7 further comprising means forpartially condensing flashed vapor from the phase separation means toprovide a recycle liquid to the first reactor stage.